EP0051888B1 - Procédé pour la purification d'eau usée et/ou de boue résiduaire - Google Patents

Procédé pour la purification d'eau usée et/ou de boue résiduaire Download PDF

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Publication number
EP0051888B1
EP0051888B1 EP19810201181 EP81201181A EP0051888B1 EP 0051888 B1 EP0051888 B1 EP 0051888B1 EP 19810201181 EP19810201181 EP 19810201181 EP 81201181 A EP81201181 A EP 81201181A EP 0051888 B1 EP0051888 B1 EP 0051888B1
Authority
EP
European Patent Office
Prior art keywords
methane fermentation
waste water
denitrification
effluent
reactor
Prior art date
Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
Expired
Application number
EP19810201181
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German (de)
English (en)
Other versions
EP0051888A1 (fr
Inventor
Arnold Mulder
Current Assignee (The listed assignees may be inaccurate. Google has not performed a legal analysis and makes no representation or warranty as to the accuracy of the list.)
Gist-Brocades Nv En Biothane Systems Internation
Original Assignee
Gist Brocades NV
Priority date (The priority date is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the date listed.)
Filing date
Publication date
Application filed by Gist Brocades NV filed Critical Gist Brocades NV
Priority to AT81201181T priority Critical patent/ATE6490T1/de
Publication of EP0051888A1 publication Critical patent/EP0051888A1/fr
Application granted granted Critical
Publication of EP0051888B1 publication Critical patent/EP0051888B1/fr
Expired legal-status Critical Current

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    • C—CHEMISTRY; METALLURGY
    • C12—BIOCHEMISTRY; BEER; SPIRITS; WINE; VINEGAR; MICROBIOLOGY; ENZYMOLOGY; MUTATION OR GENETIC ENGINEERING
    • C12M—APPARATUS FOR ENZYMOLOGY OR MICROBIOLOGY; APPARATUS FOR CULTURING MICROORGANISMS FOR PRODUCING BIOMASS, FOR GROWING CELLS OR FOR OBTAINING FERMENTATION OR METABOLIC PRODUCTS, i.e. BIOREACTORS OR FERMENTERS
    • C12M47/00—Means for after-treatment of the produced biomass or of the fermentation or metabolic products, e.g. storage of biomass
    • C12M47/18—Gas cleaning, e.g. scrubbers; Separation of different gases
    • C—CHEMISTRY; METALLURGY
    • C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F3/00—Biological treatment of water, waste water, or sewage
    • C02F3/28—Anaerobic digestion processes
    • C—CHEMISTRY; METALLURGY
    • C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F3/00—Biological treatment of water, waste water, or sewage
    • C02F3/30—Aerobic and anaerobic processes
    • C02F3/302—Nitrification and denitrification treatment
    • C—CHEMISTRY; METALLURGY
    • C12—BIOCHEMISTRY; BEER; SPIRITS; WINE; VINEGAR; MICROBIOLOGY; ENZYMOLOGY; MUTATION OR GENETIC ENGINEERING
    • C12M—APPARATUS FOR ENZYMOLOGY OR MICROBIOLOGY; APPARATUS FOR CULTURING MICROORGANISMS FOR PRODUCING BIOMASS, FOR GROWING CELLS OR FOR OBTAINING FERMENTATION OR METABOLIC PRODUCTS, i.e. BIOREACTORS OR FERMENTERS
    • C12M21/00—Bioreactors or fermenters specially adapted for specific uses
    • C12M21/04—Bioreactors or fermenters specially adapted for specific uses for producing gas, e.g. biogas
    • Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
    • Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
    • Y02E—REDUCTION OF GREENHOUSE GAS [GHG] EMISSIONS, RELATED TO ENERGY GENERATION, TRANSMISSION OR DISTRIBUTION
    • Y02E50/00—Technologies for the production of fuel of non-fossil origin
    • Y02E50/30—Fuel from waste, e.g. synthetic alcohol or diesel
    • Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
    • Y10—TECHNICAL SUBJECTS COVERED BY FORMER USPC
    • Y10S—TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
    • Y10S210/00—Liquid purification or separation
    • Y10S210/902—Materials removed
    • Y10S210/903—Nitrogenous

Definitions

  • the invention is relating to a process for the purification of waste water and/or waste water sludge, comprising subjecting the waste water and/or the waste water sludge to methane fermentation and oxidizing the reduced compounds present in the liquid effluent of the methane fermentation by aeration.
  • the COD present in the waste water (sludge) is converted for the major part into methane and carbon dioxide, while hydrogen sulphide and ammonia-originate from the sulphur containing compounds and nitrogen containing compounds respectively.
  • the hydrogen sulphide turns up in part in the methane gas and must be removed therefrom before the methane gas can be used for the energy production, while the remainder is found in the liquid effluent of the methane fermentation, in the form of unsoluble precipitates and as dissolved H 2 S and/or HS- ions.
  • the ammonia dissolves mainly in the liquid effluent of the methane fermentation.
  • liquid effluent of the methane fermentation is not appropriate for a direct draining; it stinks and is poisonous.
  • the organic compounds dissolved in the effluent are partially degraded by aeration or are converted into sludge, which is removed and for instance is recirculated to the methane fermentation, by which means the COD of that effluent is decreased significantly and the sulphides and ammonia are oxidized into sulphate ions and nitrate ions respectively.
  • the aerated water is drained off the so formed nitrate gives rise to problems with the eutrofication of surface water if waste water and/or waste water sludge having a high content of nitrogen containing compounds are used.
  • the nitrate in the aerated effluent of the methane fermentation is converted under practical conditions into nitrogen in the usual way (see for instance J.A.W.W.A., 659-662 (1969)) under anaerobic conditions in the presence of the naturally occurring denitrificat- ing microorganisms and under application of organic compounds (methanol) as electron donor (so called denitrification).
  • the obtained nitrogen is removed.
  • the ammonia from the methane fermentation is still present; this ammonia is subsequently oxidized into nitrate by aeration, whereby the sulphide cannot disturb as this was already converted into in the denitrification step.
  • the aeration needs less air and the aeration may be more simple.
  • the hydrogen sulphide from the gas which is formed during methane fermentation also can serve as electron donor in the denitrification and is preferably applied for this purpose. In this way the best possible use of the products obtained in the methane fermentation can be made while in addition the gas is purified in a simple way.
  • the effluent from the aeration step containing nitrate ions and SOQ- ions already formed during denitrification suitably is recycled in part to the denitrification step.
  • the nitrate containing effluent which is formed during the aeration, is partially subjected to the denitrification as a nitrate containing waste water, according to the invention and whereby the remainder is drained off.
  • S02- ions present in the liquid do not disturb denitrification of nitrate ions by sulphide, since sulphide is unable to reduce the ions.
  • a purification of waste water and/or waste water sludge, wherein nitrogen and sulphur containing impurities are present is achieved and, due to the methane fermentation of the COD of the waste water and/or the waste water sludge methane gas is obtained, which may serve as a source of energy.
  • the liquid effluent. and the gas of the methane fermentation as source of H 2 S, HS- and/or S 2 -, which serve as electron donors for the denitrification a reliable, economical removal of nitrogen- and reduced sulphur compounds is reached.
  • the total amount of nitrogen, which is removed, depends on the volume ratio. between the nitrate containing effluent, which is subjected to the denitrification, and the effluent of the methane fermentation, which is directed to the denitrification.
  • this volume ratio is at least 1:1. In this case at least 50% of the nitrogen is removed. Most preferably the indicated ratio is 4:1 to 9:1, because the amount of nitrogen, calculated on the basis of the waste water and/or waste water sludge, which will be removed within these ratios, namely 80 to 90%, will suffice for practical purposes.
  • one or more of these steps of this process are carried out preferably in the so called biologically fluidized bed reactor, wherein the biomass grows attached to a solid heavy carrier and thus is not leaving the reactor under high flow rate conditions.
  • Such a biomass attached to a heavy carrier system may be prepared e.g. by a process of the EP-A-0 028 846, the relevant parts of which are incorporated herein by reference.
  • nitrate containing waste waster is supplied by means of pipeline 1 to the denitrification reactor 2 having an upgoing liquid flow (up-flow reactor).
  • the liquid effluent of the methane fermentation of waste water and/or waste water sludge with N and S containing impurities is pumped by means of pipeline 3 to the reactor 2.
  • H 2 S containing gas, derived from the methane fermentation, is pumped by means of pipeline 4 into the bottom of an absorption column 5, wherein in the upper part the liquid effluent from the denitrification reactor 2 is supplied through pipeline 6.
  • the liquid wherein the H 2 S is absorbed leaves the absorption column 5 via pipeline 8 and is added to the liquid effluent of the methane fermentation in pipeline 3.
  • nitrate is reduced to nitrogen, which evades via pipeline 9.
  • This amount of purified waste water is equal to the amount of nitrate containing waste water, which is supplied by pipeline 1 together with the amount of liquid effluent of the methane fermentation which is supplied by pipeline 3.
  • the waste water and/or waste water sludge containing besides the COD nitrogen- and sulphur compounds, is supplied by means of pipeline 11 to a methane fermentation reactor 12. From this reactor ammonia and sulphide containing liquid effluent is supplied by means of pipeline 13 to a denitrification reactor 15, to which on the other hand nitrate containing waste water from the subsequent stage is added via pipeline 16 and via pipeline 17 non-purified COD containing waste water, coming from pipeline 11, are added.
  • a gas stream containing C0 21 CH 4 and H Z S which is formed in the methane fermentation is supplied by means of pipeline 14 to a washing column 24, wherein the H 2 S is removed from the gas by washing with denitrified waste water which is supplied by pipeline 25.
  • the gas from which H 2 S is removed evades from the washing column 24 by means of the pipeline 26 and the washing liquid wherein H 2 S has been absorbed is led by means of pipeline 27 into the pipeline 17 and from there to the denitrification reactor 15.
  • the denitrification reactor the nitrate, which is present in the liquid mixture, is reduced to nitrogen which evades by means of pipeline 18.
  • Denitrificated effluent which contains ammonia, originating from the effluent of the methane fermentation and sulphate, formed by the denitrification from sulphide, is led to an aerobic reactor 20 by means of pipeline 19.
  • oxygen for the oxidation of the ammonia is supplied by means of pipeline 21.
  • Nitrificated effluent leaves the reactor 20 by means of pipeline 23. A part of this effluent is drained away as purified water, the remaining part is recirculated by means of pipeline 16 to the denitrification reactor 15.
  • nitrate solution 400 mg nitrate nitrogen/I; volume 40 I/d; total amount of nitrate 1140 mmol N0 3 /d).
  • the liquid in the denitrification reactor was stirred with 2 rpm; in the reactor the pH was 7.3-7.4 and the temperature varied between 20 and 30°C.
  • the effluent from the reactor contained a negligible amount of nitrate and 400 mg SO 2- 4 /I.
  • the methane fermentation reactor 12 was prepared for the experiment by passing through during three months waste water containing COD, nitrogen compounds and sulphur compounds in an amount of 50 I per day.
  • this reactor contained 330 g of sludge, calculated as organic material.
  • the denitrification reactor 15 was prepared in the following way. It was filled half way with active sludge originating from the aeration basin of the "R.W.Z.I.” (municipal waste water- treatment plant) in Renkum-Wageningen, whereupon it was filled up with effluent from a methane fermentation reactor. After two days 2 I liquid was withdrawn from the reactor, and the reactor was filled up again with fresh effluent from the methane fermentation reactor. These manipulations were continued during one month, whereafter a continuous flow from the methane fermentation reactor was passed through beginning with an amount of 10 I/d. Thereafter the amount passed through was regularly increased during one month to 50 I/d (residence time, 3.1 h).
  • the nitrification reactor 20 was prepared by introduction of 7.5 I of liquid sludge from the aeration basin of the "R.W.Z.I.” in Renkum-Wageningen. At the end of the experiment the reactor contained 50 g of sludge, calculated as dry organic material.
  • a nitrite containing solution (333 g NaNOg/kg) was fed in the reactor 2 through pipeline 1 at a rate of 1 I/h.
  • sulfide containing stinking waste water originating from a waste water methane reactor
  • the sulfide concentration in this waste water was about 150 mg S 2- /I.
  • the pH of reactor 2 was maintained at 7.6-7.8 and the temperature was maintained at 35°C.
  • the biomass concentration in the biomass coated sand fluidized bed in reactor 2 was about 35-40 g of volatile suspended solids per kg.
  • the purified, odourless waste water flowing through pipeline 10 contained above 450 mg SO 2- 4 /I.
  • the gas production through pipeline 9 averaged about 1200 I/d and the composition of the gas was 65% N 2 , 20% CH 4 and 15% CO 2 ,
  • the denitrification capacity can thus be estimated at 2.5 kg N 2 /m 3 reactor volume/d.

Claims (6)

1. Procédé pour la purification d'eau usée et/ou de boue résiduaire, dans lequel l'eau usée et/ou la boue résiduaire est/sont soumis(es) à une fermentation méthanique et les composés réduits en présence dans l'effluent liquide de la fermentation méthanique sont oxydés par aération, caractérisé en ce que les sulfures de l'effluent de la fermentation méthanique sont utilisés comme donneurs d'électrons à un stade de dénitrification ultérieur et les composés réduits restants de l'effluent liquide de la fermentation méthanique ne sont oxydés qu'ensuite par aération.
2. Procédé suivant la revendication 1, caractérisé en ce que le H2S contenu dans le gaz formé pendant la fermentation méthanique est également utilisé comme donneur d'électrons au stade de dénitrification.
3. Procédé suivant la revendication 1 ou 2, caractérisé en ce qu'un éffluent contenant du nitrate formé pendant l'aération est recyclé pour partie au stade de dénitrification et la partie restante est rejetée.
4. Procédé suivant la revendication 3, caractérisé en ce que le rapport volumique de l'effluent contenant du nitrate, qui est soumis à la dénitrification, à l'effluent de la fermentation méthanique, qui est recyclé à la dénitrification, est d'au moins 1:1.
5. Procédé suivant la revendication 4, caractérisé en ce que le rapport volumique est de 4:1 à 9:1.
6. Procédé suivant la revendication 5, caractérisé en ce que la dénitrification est exécutée dans un réacteur dans lequel la boue activée est fixée sur un support solide pesant qui ne quitte pas le réacteur dans des conditions d'écoulement rapide.
EP19810201181 1980-11-07 1981-10-30 Procédé pour la purification d'eau usée et/ou de boue résiduaire Expired EP0051888B1 (fr)

Priority Applications (1)

Application Number Priority Date Filing Date Title
AT81201181T ATE6490T1 (de) 1980-11-07 1981-10-30 Verfahren zum reinigen von abwasser und/oder abwasserschlamm.

Applications Claiming Priority (2)

Application Number Priority Date Filing Date Title
NL8006094 1980-11-07
NL8006094A NL8006094A (nl) 1980-11-07 1980-11-07 Werkwijze voor het zuiveren van afvalwater en/of afvalwaterslib.

Publications (2)

Publication Number Publication Date
EP0051888A1 EP0051888A1 (fr) 1982-05-19
EP0051888B1 true EP0051888B1 (fr) 1984-03-07

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EP19810201181 Expired EP0051888B1 (fr) 1980-11-07 1981-10-30 Procédé pour la purification d'eau usée et/ou de boue résiduaire

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US (1) US4384956A (fr)
EP (1) EP0051888B1 (fr)
JP (1) JPS57110395A (fr)
AT (1) ATE6490T1 (fr)
DE (1) DE3162532D1 (fr)
DK (1) DK158208C (fr)
ES (1) ES506909A0 (fr)
GR (1) GR76298B (fr)
IE (1) IE52303B1 (fr)
NL (1) NL8006094A (fr)
PT (1) PT73873B (fr)

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Also Published As

Publication number Publication date
JPS57110395A (en) 1982-07-09
ATE6490T1 (de) 1984-03-15
GR76298B (fr) 1984-08-04
DK158208B (da) 1990-04-09
IE812600L (en) 1982-05-07
JPS6216717B2 (fr) 1987-04-14
DK491981A (da) 1982-05-08
NL8006094A (nl) 1982-06-01
PT73873A (en) 1981-11-01
ES8300069A1 (es) 1982-10-01
IE52303B1 (en) 1987-09-02
PT73873B (en) 1983-01-25
EP0051888A1 (fr) 1982-05-19
DE3162532D1 (en) 1984-04-12
DK158208C (da) 1990-09-03
US4384956A (en) 1983-05-24
ES506909A0 (es) 1982-10-01

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